CN104072328B - A kind of rectifier unit and rectificating method of producing for vinyltoluene - Google Patents
A kind of rectifier unit and rectificating method of producing for vinyltoluene Download PDFInfo
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Abstract
The invention discloses a kind of rectifier unit and the rectificating method of producing for vinyltoluene in chemical production technical field, its device comprises dehydrogenation liquid storage tank, polymerization inhibitor agitator tank, de-light fractionating column, lightness-removing column top condenser, lightness-removing column top return tank, rectifying column, rectifying tower top condenser, rectifying tower top return tank, the first and second benzene recovery towers, reclaim overhead condenser, reclaim return tank of top of the tower, tail gas condenser, vavuum pump, dehydrogenation liquid is sloughed light component by de-light fractionating column and is obtained finished product by rectifying column rectifying again, the first and second benzene in light component are through the first and second benzene recovery tower recyclings. in the time producing, by controlling de-light fractionating column, rectifying column, tower top temperature, pressure and the column bottom temperature of the first and second benzene recovery towers, pressure, make vinyltoluene yield high, finished product vinyltoluene purity is greater than 99%, refining once through yield is greater than 65%, meanwhile, and by the first and second benzene recyclings.
Description
Technical field
The present invention relates to a kind of chemical production equipment, particularly a kind of process units of vinyltoluene.
Background technology
Vinyltoluene is the mixture of contraposition and meta-isomer, fusing point-82.5 DEG C, 171.45 DEG C of boiling points. Density0.8970g/cm3, easily polymerization, also can with other monomer copolymerization.
English name: VinylToluene
Molecular weight: 118.18
Molecular formula: C-9H10
Structural formula:
Vinyltoluene is usually used in replacing styrene, is the low volatilization monomer of low toxicity, and character with phenylethylene seemingly, is used for preparingResin, plastics, rubber and coating etc., can improve resin properties. Be widely used in cold coating, composite, etheneIn base resin and VPI insulating impregnating varnish.
In prior art, vinyltoluene utilizes following two kinds of methods to be prepared: one, first makes toluene with etheneHydrocarbonylation generates the mixture of ethyltoluene three kinds of isomers, then divides ortho isomer, then dehydrogenation and obtaining. In certain embodimentsIn need to use dehydrogenation reactor, in dehydrogenation reaction, also need to consume a large amount of heat energy and steam, how reasonable disposition reactionDevice and heat exchanger, can more rationally utilize heat resource, becomes the technical problem of being badly in need of solution in industry. It two is first to makeToluene and acetylene reaction generate xylyl ethane, then hot tearing and obtaining. Its weak point is: ethene normal temperature is dangerous gasBody, equipment requirement is high, poor safety performance; Use the yield of acetylene reaction low.
Summary of the invention
One of object of the present invention is to provide a kind of rectifier unit of producing for vinyltoluene, can be by rectifyingMode is separated vinyltoluene from the mixed material first ethylbenzene dehydrogenation reaction, and product yield is high.
The object of the present invention is achieved like this: a kind of rectifier unit of producing for vinyltoluene, comprising:
Dehydrogenation liquid storage tank: the dehydrogenation liquid coming for storing first Ethylbenzene hydrogen removal system; Its outlet connects through lightness-removing column feed pumpDehydrogenation liquid preheater, the outlet of dehydrogenation liquid preheater is divided into two-way, and a road connects de-light fractionating column middle part, and another road is connected to inhibitionDehydrogenation liquid import on agent agitator tank;
Polymerization inhibitor agitator tank: its tank body top is provided with polymerization inhibitor import and the import of dehydrogenation liquid, is provided with in polymerization inhibitor agitator tankStirring vane, the bottom of polymerization inhibitor agitator tank connects polymerization inhibitor head tank; Polymerization inhibitor head tank bottom is divided into four tunnels, and the first via connectsReceive dehydrogenation liquid storage tank, the second road is connected to lightness-removing column top return tank, and Third Road is connected to rectifying tower top return tank, and Si road connectsReceive the first and second benzene return tanks;
De-light fractionating column: vertical setting, its tower top is divided into two-way, and the tube side that a road is connected to lightness-removing column top condenser entersMouthful, another road is connected to lightness-removing column backflow delivery side of pump; At the bottom of the tower of de-light fractionating column, be connected to rectifying column through lightness-removing column discharging pumpMiddle part;
Lightness-removing column top condenser: horizontal setting, its tube side outlet is divided into upper and lower two-way, and upside one tunnel connects tail gas condenserTube side import, downside one tunnel connects lightness-removing column top return tank;
Lightness-removing column top return tank: bottom connects the import of lightness-removing column reflux pump; Lightness-removing column backflow delivery side of pump is divided into two-way,One road is connected to the refluxing opening at de-light fractionating column top, and another road is connected to the charging aperture at the first and second benzene recovery tower middle parts;
Rectifying column: vertical setting; Its tower top is divided into two-way, and a road connects the tube side import of rectifying tower top condenser, anotherRoad is connected to rectifying column backflow delivery side of pump; At the bottom of its tower, be connected to tar tank;
Rectifying tower top condenser: horizontal setting, its tube side outlet is divided into upper and lower two-way, and it is cold that upside one tunnel connects described tail gasCondenser import, downside one tunnel connects rectifying tower top return tank;
Rectifying tower top return tank: bottom is connected to the import of rectifying column reflux pump, described rectifying column backflow delivery side of pump oneRoad is connected to the tower top of rectifying column, and another road is connected to finished product storage tank;
The first and second benzene recovery towers: vertical setting; Its tower top is divided into two-way, and the tube side that a road connects recovery overhead condenser entersMouthful, another road is connected to recovery tower backflow delivery side of pump; At the bottom of its tower, be connected to the import of dehydrogenation system through the first and second benzene rear pumps;
Reclaim overhead condenser: horizontal setting, its tube side outlet is divided into upper and lower two-way, and it is cold that upside one tunnel connects described tail gasCondenser import, downside one tunnel connects reclaims return tank of top of the tower;
Reclaim return tank of top of the tower: bottom is connected to the import of recovery tower reflux pump, described recovery tower backflow delivery side of pump oneRoad is connected to the tower top of the first and second benzene recovery towers, and another road is connected to solvent naphtha storage tank;
Tail gas condenser: the outlet of its tube side is connected to vacuum buffer tank, vacuum buffer pot bottom is connected to dehydrogenation systemOil water separator, vacuum buffer tank top connects the import of vavuum pump;
Vavuum pump: atmosphere or incinerator are connected in outlet after the shell side of tail gas post-condenser; Tail gas post-condenser bottomShell side outlet of another road after gas-liquid separator, be connected to the oil water separator of dehydrogenation system.
The invention provides the technical scheme of the liquid after first ethylbenzene dehydrogenation being carried out to rectifying acquisition vinyltoluene, this dressWhile putting work, slough low-boiling light component by de-light fractionating column, then by rectifying column, vinyltoluene is steamed, colderSolidifying recovery obtains vinyltoluene, light component again through the first and second benzene recovery towers by the first and second benzene recyclings. In said process, inhibitionAgent constantly feeds polymerization inhibitor in dehydrogenation liquid storage tank, lightness-removing column top return tank, rectifying tower top return tank, avoids polymerisation; LogicalThe design of crossing lightness-removing column top condenser and reclaiming overhead condenser, by the first and second benzene in the light component being distilled out of in de-light fractionating columnReclaim; Design by rectifying tower top condenser and rectifying tower top return tank obtains finished product; Lightness-removing column top condenser, recovery tower topCondenser and rectifying tower top condenser share tail gas condenser, vavuum pump and a tail gas post-condenser, can be by the first in tail gasEthylbenzene and a small amount of aromatic hydrocarbons further reclaim, and not only reusable edible, meanwhile, has reduced discharge. This device makes vinyltolueneYield is high, and finished product vinyltoluene purity is large. This device is exclusively used in the first and second benzene dehydrogenations and manufactures in the production of vinyltoluene.
As a further improvement on the present invention, described de-light fractionating column, rectifying column and the first and second benzene recovery tower sides are respectively alsoConnection is provided with the heat exchanger that boils again, then reclaim with corresponding de-light fractionating column, rectifying column and the first and second benzene the tube side upper end of the heat exchanger that boilsTower bottom is connected, then the bottom of the heat exchanger tube pass that boils and the corresponding bottom that takes off light fractionating column, rectifying column and the first and second benzene recovery towersFluid pipeline is connected. Boil heat exchanger as the thermal source that takes off material in light fractionating column and rectifying column, de-light fractionating column and rectifying column againInterior liquid enters the heat exchanger that boils again and is heated and partial gasification, and the material now boiling again in heat exchanger becomes liquid-vapor mixture, closeDegree has diminished, and fluid density in tower body is larger, and liquid flows into by density contrast the heat exchanger that boils again, forms circulation.
As a further improvement on the present invention, described tar tank bottom connects detar still, the gas at detar still topOutlet connects the tube side import of decoking kettle condenser, and detar still bottom is provided with tar outlet; The tube side of decoking kettle condenser goes outMouth is divided into two-way, and a road connects tail gas condenser, and another road connects decoking flow container, and the outlet of decoking liquid pot bottom is connected to described de-Hydrogen liquid storage tank. This structure is processed tar, makes vinyltoluene be wherein further recovered to dehydrogenation liquid storage tank, carries outRectifying again, has improved the yield of vinyltoluene product.
As a further improvement on the present invention, described rectifying tower top condenser, decoking kettle condenser, recovery overhead condenserTube side outlet also have a roadside to lead to connect vacuum buffer tank. This scheme makes ensureing yield and discharging satisfactory situationUnder, partial tail gas can directly be walked around tail gas condenser, makes management, more convenient operation.
For ensureing reliable operation, described lightness-removing column feed pump has been arranged in parallel two groups; Vacuum buffer tank and vavuum pump are also alsoConnection is provided with two groups. Two groups for subsequent use each other, improved the reliability of system works.
The present invention also provides a kind of rectificating method for this production of vinyltoluene, and it is above-mentioned for vinyltolueneThe rectifier unit of producing carries out rectifying, and wherein 88 ~ 90 DEG C of tower top temperatures, the pressure of de-light fractionating column are 1.9 ~ 2.1KPa, de-lightFractionating column tower bottom outlet temperature is 90 ~ 100 DEG C, pressure 5.8 ~ 6.2KPa; Rectifying column tower top temperature is that 90 ~ 93 DEG C, pressure are 1.9~ 2.1KPa, at the bottom of the tower of rectifying column, discharging opening temperature is that 89 ~ 91 DEG C, pressure are 5.8 ~ 6.2KPa; The first and second benzene recovery tower tower top temperatures68 ~ 70 DEG C, pressure are 1.9 ~ 2.1KPa, and the first and second benzene recovery tower tower bottom outlet temperature are 90 ~ 100 DEG C, pressure 5.8 ~ 6.2KPa. LogicalCross and control corresponding parameter and make vinyltoluene yield high, finished product vinyltoluene purity is greater than 99%, and refining once through yield is largeIn 65%, meanwhile, the fully recycling of the first and second benzene.
For reducing polymerisation, reflux at dehydrogenation liquid storage tank, lightness-removing column top return tank, rectifying tower top return tank and the first and second benzeneTank domestic demand constantly adds polymerization inhibitor, polymerization inhibitor adopt arbitrary proportion 2,4-DNP and/or to tert-butyl o benzene twoPhenol, the clean quality addition of polymerization inhibitor is to enter 0.01% ~ 0.3% of the interior liquid quality flow of corresponding tank body.
As a further improvement on the present invention, entering dehydrogenation liquid in polymerization inhibitor agitator tank and the mass ratio of polymerization inhibitor is 20~ 40. Dehydrogenation liquid and polymerization inhibitor mix, and Main Function is to dilute polymerization inhibitor.
Brief description of the drawings
Fig. 1 is process chart of the present invention.
Wherein, D102 dehydrogenation liquid storage tank, P102a, P102b lightness-removing column feed pump, E200 dehydrogenation liquid preheater, D401 inhibitionAgent agitator tank, D402 polymerization inhibitor head tank, T201 takes off light fractionating column, P202 lightness-removing column discharging pump, the heat exchange of boiling again of E201 lightness-removing columnDevice, E202 lightness-removing column top condenser, D201 lightness-removing column top return tank, P201 lightness-removing column reflux pump, E205 decoking kettle condenser,D205 decoking flow container, the E203 rectifying column heat exchanger that boils again, F201 detar still, T202 rectifying column, D202 tar tank, E204 rectifyingOverhead condenser, D203 rectifying tower top return tank, P203 rectifying column reflux pump, the E206 recovery tower heat exchanger that boils again, T203 first and secondBenzene recovery tower, P205 the first and second benzene rear pumps, E207 reclaims overhead condenser, and D204 reclaims return tank of top of the tower, and P204 recovery tower returnsStream pump, E208 tail gas condenser, D208a, D208b vacuum buffer tank, M201a, M201b vavuum pump, condensation after E209 tail gasDevice, D207 gas-liquid separator.
Detailed description of the invention
As shown in Figure 1, be a kind of rectifier unit of producing for vinyltoluene, its structure mainly comprises:
Dehydrogenation liquid storage tank D102: the dehydrogenation liquid coming for storing first Ethylbenzene hydrogen removal system; It exports through lightness-removing column feed pumpConnect dehydrogenation liquid preheater E200, dehydrogenation liquid preheater E200 outlet is divided into two-way, and a road connects de-light fractionating column T201 middle part,Another road is connected to the dehydrogenation liquid import on polymerization inhibitor agitator tank D401; Lightness-removing column feed pump has been arranged in parallel two groups, is respectivelyLightness-removing column feed pump P102a, lightness-removing column feed pump P102b.
Polymerization inhibitor agitator tank D401: its tank body top is provided with polymerization inhibitor import and the import of dehydrogenation liquid, polymerization inhibitor agitator tankIn D401, be provided with stirring vane, the bottom of polymerization inhibitor agitator tank D401 connects polymerization inhibitor head tank D402; Polymerization inhibitor head tankD402 bottom is divided into four tunnels, and the first via is connected to dehydrogenation liquid storage tank D102, and the second road is connected to lightness-removing column top return tank D201, theThree roads are connected to rectifying tower top return tank D203, and Si road is connected to the first and second benzene return tanks;
De-light fractionating column T201: vertical setting, its tower top is divided into two-way, and a road is connected to lightness-removing column top condenser E202'sTube side import, another road is connected to the outlet of lightness-removing column reflux pump P201; At the bottom of the tower of de-light fractionating column T201 through lightness-removing column dischargingPump P202 is connected to the middle part of rectifying column T202;
Lightness-removing column top condenser E202: horizontal setting, its tube side outlet is divided into upper and lower two-way, and it is cold that upside one tunnel connects tail gasThe import of condenser E208 tube side, downside one tunnel connects lightness-removing column top return tank D201;
Lightness-removing column top return tank D201: bottom connects the import of lightness-removing column reflux pump P201; Lightness-removing column reflux pump P201'sOutlet is divided into two-way, and a road is connected to the refluxing opening at de-light fractionating column T201 top, and another road is connected to the first and second benzene recovery towersThe charging aperture at T203 middle part;
Rectifying column T202: vertical setting; Its tower top is divided into two-way, and the tube side that a road connects rectifying tower top condenser E204 entersMouthful, another road is connected to the outlet of rectifying column reflux pump P203; At the bottom of its tower, be connected to tar tank D202;
Rectifying tower top condenser E204: horizontal setting, its tube side outlet is divided into upper and lower two-way, and upside one tunnel connects described tailGas condenser E208 import, downside one tunnel connects rectifying tower top return tank D203;
Rectifying tower top return tank D203: bottom is connected to the import of rectifying column reflux pump P203, described rectifying column reflux pumpOutlet one road of P203 is connected to the tower top of rectifying column T202, and another road is connected to finished product storage tank;
The first and second benzene recovery tower T203: vertical setting; Its tower top is divided into two-way, and a road connects reclaims overhead condenser E207'sTube side import, another road is connected to the outlet of recovery tower reflux pump P204; At the bottom of its tower, be connected to de-through the first and second benzene rear pump P205The import of hydrogen system;
Reclaim overhead condenser E207: horizontal setting, its tube side outlet is divided into upper and lower two-way, and upside one tunnel connects described tailGas condenser E208 import, downside one tunnel connects reclaims return tank of top of the tower D204;
Reclaim return tank of top of the tower D204: bottom is connected to the import of recovery tower reflux pump P204, described recovery tower reflux pumpOutlet one road of P204 is connected to the tower top of the first and second benzene recovery tower T203, and another road is connected to solvent naphtha storage tank;
Tail gas condenser E208: its tube side outlet is connected to vacuum buffer tank, and vacuum buffer pot bottom is connected to dehydrogenation systemThe oil water separator of system, vacuum buffer tank top connects the import of vavuum pump;
Vavuum pump: atmosphere or incinerator are connected in outlet after the shell side of tail gas post-condenser E209; Tail gas post-condenserAnother road shell side outlet of E209 bottom is connected to the oil water separator of dehydrogenation system after gas-liquid separator D207.
Above-mentioned vacuum buffer tank and vavuum pump have been arranged in parallel two groups, are respectively vacuum buffer tank D208a and D208b, trueEmpty pump M201a and M201b.
De-light fractionating column T201, rectifying column T202 and the first and second benzene recovery tower T203 sides have been arranged in parallel respectively the heat exchange of boiling againDevice, is respectively lightness-removing column heat exchanger E201, rectifying column heat exchanger E203, the recovery tower heat exchanger E206 that boils again that boils again that boils again, then boilsThe tube side upper end of heat exchanger is connected with the first and second benzene recovery tower T203 bottoms with corresponding de-light fractionating column T201, rectifying column T202,Boil the again bottom of heat exchanger tube pass and the bottom of corresponding de-light fractionating column T201, rectifying column T202 and the first and second benzene recovery tower T203Fluid pipeline is connected.
Tar tank D202 bottom connects detar still F201, and it is cold that the gas vent at detar still F201 top connects decoking kettleThe tube side import of condenser E205, detar still F201 bottom is provided with tar outlet; The tube side outlet point of decoking kettle condenser E205Become two-way, a road connects tail gas condenser E208, and another road connects decoking flow container D205, and decoking flow container D205 outlet at bottom connectsTo described dehydrogenation liquid storage tank D102.
The tube side outlet of rectifying tower top condenser E204, decoking kettle condenser E205, recovery overhead condenser E207 also hasOne roadside is led to and is connect vacuum buffer tank.
When this device work, in polymerization inhibitor agitator tank D401, add polymerization inhibitor, the dehydrogenation liquid that itself and dehydrogenation liquid preheater comeMix, then respectively to dehydrogenation liquid storage tank D102, lightness-removing column top return tank D201, rectifying tower top return tank D203, recoveryIn tower return tank D204, constantly feed a certain amount of polymerization inhibitor, to reduce the generation of polymerisation, polymerization inhibitor adopts arbitrary proportion2,4-DNP and/or p-tert-butyl catechol, as independent selection 2,4-DNP; Or select separately rightTert-butyl catechol; Also can both mass ratioes of choice for use each 50%; Or a kind of quality 10%, another kind of quality 90% selected; ResistanceThe clean quality addition of poly-agent is to enter 0.05% ~ 0.3% of the interior liquid quality flow of corresponding tank body, and this flow is moment flow.The dehydrogenation liquid that first ethylbenzene dehydrogenation reaction generates leaves in dehydrogenation liquid storage tank D102, and the main component of this dehydrogenation liquid is: the first and second benzene,Vinyltoluene, n-proplbenzene, isopropylbenzene and ortho-xylene, wherein the first and second benzene account for that weight ratio is 40 ~ 45%, vinyltoluene 45 ~50%, wherein the boiling point under vinyltoluene normal pressure is the highest, wherein 88 ~ 90 DEG C of tower top temperatures, the pressure of de-light fractionating column be 1.9 ~2.1KPa, can slough light component, and de-light fractionating column tower bottom outlet temperature is 90 ~ 100 DEG C, pressure 5.8 ~ 6.2KPa; Rectifying columnTower top temperature is that 90 ~ 93 DEG C, pressure are 1.9 ~ 2.1KPa, at the bottom of the tower of rectifying column discharging opening temperature be 89 ~ 91 DEG C, pressure be 5.8 ~6.2KPa; The first and second 68 ~ 70 DEG C of benzene recovery tower tower top temperatures, pressure are 1.9 ~ 2.1KPa, the first and second benzene recovery tower tower bottom outlet temperatureBe 90 ~ 100 DEG C, pressure 5.8 ~ 6.2KPa. Vacuum in de-light fractionating column T201, rectifying column T202, the first and second benzene recovery tower T203Degree is controlled by vavuum pump M201a or vavuum pump M201b, and temperature is boiled and changed again by boil again heat exchanger E201, rectifying column of lightness-removing columnHot device E203, the recovery tower heat exchanger E206 that boils again controls, and the cut at de-light fractionating column T201 top is by lightness-removing column top condenserAfter E202 condensation, enter lightness-removing column top return tank D201, after collection, go the first and second benzene recovery towers to carry out recycling; Rectifying towerThe cut on top enters rectifying tower top return tank D203 after by rectifying tower top condenser E204 condensation, and capable of circulation time rectifying column carries outEvaporate again, reach after requirement until its rectifying purity, can be transported to finished product storage tank by rectifying column reflux pump P203. At vavuum pumpTail gas condenser E208 is set before M201a, M201b, and tail gas post-condenser E209 after vavuum pump, is ensureing that vacuum meets the requirementsSituation under, can be to greatest extent by tail gas recycle; Ensureing yield and discharging in satisfactory situation, partial tail gas canDirectly walk around tail gas condenser E208; The tail gas reclaiming can be sent into circulation point again in the oil water separator of dehydrogenation system againFrom, a small amount of on-condensible gas is direct emptying or burn clean. The tar of rectifying column T202 bottom is collected and deposits after treatment.
The present invention is not limited to above-described embodiment, on the basis of technical scheme disclosed by the invention, and the skill of this areaArt personnel, according to disclosed technology contents, do not need performing creative labour just can make one to some technical characterictics whereinA little replacement and distortion, these replacements and distortion are all in protection scope of the present invention.
Claims (8)
1. a rectifier unit of producing for vinyltoluene, is characterized in that comprising
Dehydrogenation liquid storage tank: the dehydrogenation liquid coming for storing first Ethylbenzene hydrogen removal system; Its outlet connects dehydrogenation through lightness-removing column feed pumpLiquid preheater, the outlet of dehydrogenation liquid preheater is divided into two-way, and a road connects de-light fractionating column middle part, and another road is connected to polymerization inhibitor and stirsMix the dehydrogenation liquid import on tank;
Polymerization inhibitor agitator tank: its tank body top is provided with polymerization inhibitor import and the import of dehydrogenation liquid, is provided with stirring in polymerization inhibitor agitator tankBlade, the bottom of polymerization inhibitor agitator tank connects polymerization inhibitor head tank; Polymerization inhibitor head tank bottom is divided into four tunnels, and the first via is connected toDehydrogenation liquid storage tank, the second road is connected to lightness-removing column top return tank, and Third Road is connected to rectifying tower top return tank, and Si road is connected toThe first and second benzene return tanks;
De-light fractionating column: vertical setting, its tower top is divided into two-way, and a road is connected to the tube side import of lightness-removing column top condenser, anotherOne road is connected to lightness-removing column backflow delivery side of pump; At the bottom of the tower of de-light fractionating column through lightness-removing column discharging pump be connected to rectifying column inPortion;
Lightness-removing column top condenser: horizontal setting, its tube side outlet is divided into upper and lower two-way, and upside one tunnel connects tail gas condenser tube sideImport, downside one tunnel connects lightness-removing column top return tank;
Lightness-removing column top return tank: bottom connects the import of lightness-removing column reflux pump; Lightness-removing column backflow delivery side of pump is divided into two-way, a roadBe connected to the refluxing opening at de-light fractionating column top, another road is connected to the charging aperture at the first and second benzene recovery tower middle parts;
Rectifying column: vertical setting; Its tower top is divided into two-way, and a road connects the tube side import of rectifying tower top condenser, and another road connectsReceive rectifying column backflow delivery side of pump; At the bottom of its tower, be connected to tar tank;
Rectifying tower top condenser: horizontal setting, its tube side outlet is divided into upper and lower two-way, and upside one tunnel connects described tail gas condenserImport, downside one tunnel connects rectifying tower top return tank;
Rectifying tower top return tank: bottom is connected to the import of rectifying column reflux pump, described rectifying column backflow delivery side of pump one tunnel connectsReceive the tower top of rectifying column, another road is connected to finished product storage tank;
The first and second benzene recovery towers: vertical setting; Its tower top is divided into two-way, and a road connects the tube side import of reclaiming overhead condenser, anotherOne road is connected to recovery tower backflow delivery side of pump; At the bottom of its tower, be connected to the import of dehydrogenation system through the first and second benzene rear pumps;
Reclaim overhead condenser: horizontal setting, its tube side outlet is divided into upper and lower two-way, and upside one tunnel connects described tail gas condenserImport, downside one tunnel connects reclaims return tank of top of the tower;
Reclaim return tank of top of the tower: bottom is connected to the import of recovery tower reflux pump, described recovery tower backflow delivery side of pump one tunnel connectsReceive the tower top of the first and second benzene recovery towers, another road is connected to solvent naphtha storage tank;
Tail gas condenser: its tube side outlet is connected to vacuum buffer tank, and vacuum buffer pot bottom is connected to the profit of dehydrogenation systemSeparator, vacuum buffer tank top connects the import of vavuum pump;
Vavuum pump: atmosphere or incinerator are connected in outlet after the shell side of tail gas post-condenser; Tail gas post-condenser bottom anotherOne road shell side outlet is connected to the oil water separator of dehydrogenation system after gas-liquid separator.
2. the rectifier unit of producing for vinyltoluene according to claim 1, is characterized in that: described de-light fractionationTower, rectifying column and the first and second benzene recovery tower sides have been arranged in parallel respectively the heat exchanger that boils again, then the tube side upper end and phase of the heat exchanger that boilsDe-light fractionating column, rectifying column and the first and second benzene recovery tower bottoms of answering are connected, then the bottom of the heat exchanger tube pass that boils is with corresponding de-lightThe bottom fluid pipeline of fractionating column, rectifying column and the first and second benzene recovery towers is connected.
3. the rectifier unit of producing for vinyltoluene according to claim 1, is characterized in that: at the bottom of described tar tankPortion connects detar still, and the gas vent at detar still top connects the tube side import of decoking kettle condenser, detar still bottomBe provided with tar outlet; The tube side outlet of decoking kettle condenser is divided into two-way, and a road connects tail gas condenser, and another road connects decokingFlow container, the outlet of decoking liquid pot bottom is connected to described dehydrogenation liquid storage tank.
4. the rectifier unit of producing for vinyltoluene according to claim 3, is characterized in that: rectifying tower top condensationDevice, decoking kettle condenser, the tube side outlet of reclaiming overhead condenser also have a roadside to lead to connect vacuum buffer tank.
5. the rectifier unit of producing for vinyltoluene according to claim 1, is characterized in that: described lightness-removing column entersMaterial parallel connection of pumps is provided with two groups; Vacuum buffer tank and vavuum pump have also been arranged in parallel two groups.
6. a rectificating method of producing for vinyltoluene, it is characterized in that utilizing described in claim 1 for etheneThe rectifier unit that base toluene is produced carries out rectifying, wherein 88 ~ 90 DEG C of tower top temperatures, the pressure of de-light fractionating column be 1.9 ~2.1KPa, de-light fractionating column tower bottom outlet temperature is 90 ~ 100 DEG C, pressure 5.8 ~ 6.2KPa; Rectifying column tower top temperature is 90 ~ 93DEG C, pressure is 1.9 ~ 2.1KPa, at the bottom of the tower of rectifying column, discharging opening temperature is that 89 ~ 91 DEG C, pressure are 5.8 ~ 6.2KPa; The first and second benzene return68 ~ 70 DEG C of receipts column overhead temperature, pressure are 1.9 ~ 2.1KPa, and the first and second benzene recovery tower tower bottom outlet temperature are 90 ~ 100 DEG C, pressure5.8~6.2KPa。
7. a kind of rectificating method of producing for vinyltoluene according to claim 6, is characterized in that the storage of dehydrogenation liquidIn tank, lightness-removing column top return tank, rectifying tower top return tank and the first and second benzene return tanks, constantly add polymerization inhibitor, polymerization inhibitor adopts arbitrarilyThe 2,4-DNP of ratio and/or p-tert-butyl catechol, the clean quality addition of polymerization inhibitor is for entering corresponding tank body0.05% ~ 0.3% of interior liquid quality flow.
8. a kind of rectificating method of producing for vinyltoluene according to claim 6, is characterized in that entering inhibitionDehydrogenation liquid in agent agitator tank and the mass ratio of polymerization inhibitor are 20 ~ 40.
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| CN106084283B (en) * | 2016-06-29 | 2019-10-01 | 新疆中泰化学股份有限公司 | Production of PVC recycling monomer processing unit and Production of PVC recycling monomer processing method |
| CN114573414A (en) * | 2020-12-01 | 2022-06-03 | 中国石化工程建设有限公司 | Device and method for removing light components in styrene monomer |
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| US4492675A (en) * | 1980-12-31 | 1985-01-08 | Cosden Technology, Inc. | Apparatus for the production of vinyltoluene |
| US4417085A (en) * | 1981-04-02 | 1983-11-22 | Cosden Technology, Inc. | Process for the production of vinyltoluene |
| CN102503762A (en) * | 2011-11-17 | 2012-06-20 | 江苏正丹化学工业股份有限公司 | Production method for vinyl toluene |
| CN203668270U (en) * | 2013-12-27 | 2014-06-25 | 江苏正丹化学工业股份有限公司 | Rectification device for vinyl toluene production |
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